METHOD AND SYSTEM FOR TREATMENT OF WATER AND WASTEWATER

Abstract: This substantially constant level biological wastewater treatment process and system enables efficient treatment of wastewater, combining the advantages and eliminating the disadvantages of both SBR and activated sludge processes. In the present case, wastewater continuously flows in one direction through a plurality of treatment cells hydraulically connected in series. The wastewater is subjected to biological treatment in at least one of the cells and settled in at least one last treatment and discharge cell, immediately prior to discharge from the system. In subsequent steps, the wastewater may continue to be fed into the system at the same location while the discharge from the last cell is temporarily closed, the mixing aeration device therein is turned on to re-suspend the settled mixed liquor suspended solids and provide additional treatment, a transfer pump therein is turned on to transfer the mixed liquor suspended solids and co-mingled partially treated wastewater back to a previous treatment cell, and at the completion of the transfer step the mixing aeration device is turned off to once again allow settling of biological solids prior to once again discharging treated wastewater on a continuing basis. Mixed liquor suspended solids flow in the same general direction as the wastewater but always receive at least partial transfer back to a prior treatment cell, settling and separation of the remaining solids from the wastewater prior to discharged of treated wastewater from the last cell. Preferred embodiments of the invention include continous discharge and essentially completely constant level operation by use of two discharge cells alternatively and treatment of soluble and particulate contaminants as well as biological removal of nitrogen and phosphorus.

Description: METHOD AND SYSTEM FOR TREATMENT OF WATER AND WASTEWATER This invention relates to a method and a system for treatment of water and wastewater. More specifically, the method and system of the present invention are designed for the biological removal from wastewater of contamination in the form of solids and soluble organic material, and optionally the biological removal of nitrogen and phosphorus nutrients. The biological treatment of sewage and other apparatuses for effecting such treatment are described in United States Patents Nos. 2,907,463, issued to D.J.N. Light et al on October 6, 1959; 3,964,998, issued to J.L. Bernard on June 22, 1976; 4,279,753 issued to N.E. Nielson et al on July 21, 1981; 4,430,224, issued to U. Fuchs on February 7, 1984; 4,468,327 issued to A.D. Brown on August 28, 1984; 4,522,722 issued to E.M. Nicholas on June 11, 1985; 4,663,044 issued to M.C. Goronszy on May 5, 1987; 4,798,673 issued to C. Huntington on January 17, 1989; 204,867,883, issued to G.T. Daigger on September 19, 1989; 4,948,510 issued to M.D. Todd et al . on August 14, 1990; 5,013,441 issued to M.C. Goronszy on May 7, 1991; and in Canadian Patents Nos. 997,488, issued to B.K. Tholander et al . on September 21, 1976 and 251,117,042, issued to M.L. Spector on January 26, 1982. In general, suspended growth activated sludge - 1 - SUBSTITUTE SHEET processes and modifications thereto have recently been shown to be able to accomplish the objectives set out above, but the costs of specialized clarifiers required to settle and recycle biological solids is quite high. Moreover, the size, complexity and operating problems encountered with such systems make them unattractive to potential users. In addition, the basic activated sludge process often results in poor treatment because of the continuous flow through characteristics in the final clarifier and the resulting constant sludge management requirements. As a consequence of the foregoing, during the past ten years improved final clarification and solids removal has been sought by using larger and improved but more complex and expensive designs for final clarifiers. Moreover, final effluent filtration is often necessary to reliably meet permitted environmental standards. There has also been a recent revival of interest in the sequencing batch reactor (SBR) suspended growth activated sludge process because of the inherently more efficient batch organic contaminants removal than is possible with the conventional continuous flow activated sludge process. The SBR process uses the same vessel for batch aerated biological reaction and quiescent batch settling. Thus, the SBR process eliminates the major cost of dedicated final clarifiers necessary for the conventional activated sludge - -> - SUBSTITUTE SHEET process as well as improving upon solids removal performance. However, the SBR process has several disadvantages, the principle one being that it does not operate with a constant level and continuous flow, but requires intermittent operation for cycles of fill, react, settle, decant and idle. Typical level fluctuations are 30% to 50% of the maximum operating depth or as much as 5 to 10 feet of level fluctuations. The result is a much lower use to total volume ratio than the conventional activated sludge process. Accordingly, the SBR process is generally not cost effective for flows greater than five to ten million gallons per day ( GD) . Another disadvantage of the SBR process is that significant head loss occurs from the influent to the final effluent, requiring additional energy and pumping costs. Additionally, because the effluent flow is not continuous, flow equalization systems may be required to prevent peak loadings and adverse impacts on receiving waters. Finally, the basic process and design limitations of the SBR process make it difficult to achieve the same high efficiency biological nutrient removal possible using the continuous flow activated sludge process, especially for weak or colder waters. Several improvements have been attempted to overcome the SUBSTITUTE SHEET limitations of the conventional activated sludge process. A continuous inflow, partitioned SBR process Patent No. 4,468,327 was issued to A.D. Brown on August 28, 1984, and cyclically operated intermittent flow path sequential cycle, multi-zoned recycle SBR process Patents # 4,663,044 and # 5,013,441 were issued to H.G. Goronszy on May 5, 1987 and May 7, 1991, respectively. Significant level fluctuations, head losses and intermittent high flow rate discharges, however, still prevent these processes from overcoming all the limitations of the conventional SBR process. Attempts have also been made over the years to overcome the level variation limitations of all SBR type processes and the cost of dedicated final clarifiers for the conventional activated sludge process. The Degremont S.A. U.S. Patent No. 3,470,092 issued to J.J.P. Bernard on September 30, 1969 illustrates a first attempt to develop a new suspended growth activated sludge process utilizing the concepts of both batch treatment and continuous flow. This two cell process was partially interconnected at the water surface. The alternate cell feed concept was not effective because it did not achieve a high treatment efficiency, had a low aerator utilization factor, and required long detention times to operate resulting in expensive systems. Union Carbide U.S. Patent No. 4,179,366 issued to J.R. Kaelin on December 18, 1979 added a third bottom - 4 - SUBSTITUTESHEET interconnected cell, but also suffered from low treatment efficiency and ineffective changeover of untreated wastewater wastewater from the first cell to the third cell. The processes disclosed by both patents also required significant level fluctuations in the treatment cells between operating cycles which made it difficult to control flows and operate fixed, level sensitive mechanical aeration systems. Linde AG German Patent No. 3,147,920 issued on October 13, 1983 utilized the same three cell concept as U.S. Patent No. 4,179,366. Although this three cell process achieved a more constant level, and overcame some of the limitations of the prior art, the process failed because it relied on expensive and unreliable mechanical gates to separate the treatment cells at various cycle times, and because treatment efficiency and effectiveness was too low to be commercially useful. VOR SA French Patent No. 2550522 issued on February 15, 1985, describes another constant level apparatus including three separate, identical basins. The process required a large, expensive treatment system because three independent basins were required, and only 1/3 of the total treatment volume was used for biological treatment at any time, and only 1/3 of the aeration equipment could be used at one time. - 5 - SUBSTITUTE SHEET In spite of these attempts to improve on the performance and effectiveness of the SBR conventional activated sludge processes, they do not provide a higher treatment efficiency and hence they are not significantly most cost effective. Such attempts have either failed to totally achieve the desired benefits, or have new inherent disadvantages which result in little or not benefits compared to conventional methods. All these attempts to develop constant level processes to improve on the conventional suspended growth activated sludge process, rely on the management control and recycle of mixed liquor suspended solids by back flushing or forward flushing through or around the treatment system by control of the timing and direction of wastewater flow into and through the treatment system. These methods of solids management differ significantly from variable level SBR's, and also differ from the constant level conventional activated sludge process, which settles the mixed liquor suspended solids in a dedicated final clarifier to collect and recycle the resulting activated sludge back to the aeration basin. In contrast, this present invention relies on biological solids management by a novel substantially constant level wastewater treatment method and system in which mixed liquor suspended solids are positively - 6 - SUBSTITUTE SHEET transferred alternatively from at least one last treatment discharge cell to a previous hydraulically connected treatment cell simultaneously with the co-mingled partially treated wastewater, while being subjected to mixing prior to each last cell sequentially functioning once again as a quiescent clarifier for discharge of final treated effluent. The novel treatment method and system makes it possible to achieve many worthwhile objectives to significantly increase the usefulness and lower the cost of wastewater treatment. The principle object of the present invention similar to the objective of applicant's co-pending United States Patent Application No. 07/963,478, filed October 19, 1992, is to provide a method and a system which maintains the benefits of the sequencing batch reactor (SBR) process while eliminating the disadvantages. Another object of the invention is to eliminate the disadvantages of prior art attempts to improve on SBR and conventional activated sludge processes by achieving greater utilization and effectiveness of the aeration systems, maintaining a constant level or requiring only small hydraulic level changes, and thus increasing the oxygen transfer efficiency of the aeration systems, and not exceeding aeration power per unit volume limitations as it is common with some process designs to date, making possible - 7 - SUBSTITUTE SHEET the use of a fixed level discharge weir flow control systems and continuous flow in, through, and out of a treatment system at all times. Another object of the invention is to provide a process that is capable of achieving a high treatment efficiency and a system which is simple to design, construct, operate and maintain, while being more cost effective than either SBR or conventional activated sludge processes for either small or large flows up to 100 MGD or greater. Another object of the invention is to provide a low cost method and a treatment system facilitating biological nitrogen and/or phosphorus nutrient removal even for weak (e.g. dilute) or colder wastewaters as is possible, but at high costs, by use of advanced nutrient removal activated sludge processes. Another another object of the invention is the use of a single basin for treatment to eliminate the inefficient land use, costs, and complexity of treating wastewaters in a plurality of separate hydraulic structures as required by SBR and conventional activated sludge processes to date. Another object of the invention is to make possible a low cost modification of existing aerated basins or lagoons to convert them to a higher treatment efficiency activated sludge process style of treatment, either by use of "on-the- run" modifications or by simple expansion of the aerated SUBSTITUTESHEET basins or lagoons. Yet another object of the invention is to be able to operate at low or high food to micro-organism ratios and at low to high hydraulic retention times, depending on the sludge age and resulting waste sludge production rate selected by a designer, as well as being able to operate for a specific system with low food to micro-organism ratio variations and hence making possible optimized system process operations and minimum treated effluent variations. A final object of the invention is to make possible the use of a single dedicated inlet location for introducing untreated wastewater into the treatment system like the conventional activated sludge process and to eliminate the operating complexity and cost of multiple controls and facilities needed to direct untreated wastewater to different treatment cells or hold back flows within the system at different time periods as is common with SBR type processes. In accordance with one aspect, the invention relates to a method of biologically treating wastewater by a modified activated sludge process comprising the following steps: feeding the wastewater at a dedicated single inlet position to a first treatment cell so the wastewater flows in the same direction through a plurality of treatment cells hydraulically connected in series; subjecting the wastewater to aeration _ 9 _ SUBSTITUTE SHEET mixing and biological treatment m at least one cell; settling the mixed liquor suspended solids in the wastewater and discharge of treated wastewater from at least one (last) treatment discharge cell while the aeration mixing means is turned off so that the settled mixed liquor suspended solids remains in the treatment systems; transferring mixed liquor suspended solids and co-mingled partially treated wastewater back to at least one previous cell to provide biological treatment therein while the discharge from the treatment discharge cell is closed and the aeration mixing means therein is turned on to re-suspend the settled mixed liquor suspended solids; and at the completion of the solids transfer step recommencing discharge of treated wastewater from the (last) discharge cell after final (batch) wastewater polishing treatment by aeration mixing and pre- settling of mixed liquor suspended solids has been completed. The method includes recycle of partially treated wastewater and biological solids contained in the mixed liquor suspended solids and a method of controlling the schedule of treated wastewater being discharged from the system in a fixed pattern selected to achieve the treatment objectives. Achieving a substantially constant water level is possible by using only one last cell for long hydraulic retention time systems. A method of achieving a substantially constant level of operation with the invention - 10 - SUBSTITUTE SHEET for even shoit hydraulic retention time systems includes controlling the flow out of two (last) treatment discharge cells, both of which are hydraulically connected to the first cell, so that they discharge alternatively. In accordance with a second aspect, the invention relates to a system for biological treatment of wastewater comprising at least two cells or zones in a basin wherein one (first ) cell is a feed cell provided with inlet means for introducing wastewater; all cells are hydraulically connected in series from the feed cell to the discharge cell(s), and are typically provided with aeration mixing means so biological treatment and mixing can be provided to the wastewater in all cells; at ]east one (last) treatment discharge cell is provided with on-off control means for its aeration mixing means, outlet flow controτl means for discharging treated wastewater out of the treatment system after the aeration mixing means is shut off to allow pre- settlmg of mixed liquor suspended solids, and « transfer means to transfer mixed liquor suspended solids and partially treated wastewater back to a prior treatment cell while said aeration mixing means is turned on; and the entire treatment system may be operated automatically by providing a central flow control means to direct the flow through and out of the treatment basin and to control the on-off schedule for said aeration mixing means, said - 11 - SUBSTITUTESHEET discharge flow control means and said transfer means to transfer mixed liquor suspended solids and partially treated wastewater back to the previous cell. Two or more last cells are provided for short hydraulic retention time systems in order to achieve substantially constant level operation. The invention will be described in greater detail, with reference to the accompanying drawings, which illustrate preferred embodiments of the system of the present invention, and wherein: Figure la is a schematic flow diagram of a two cell long hydraulic retention time system for providing biological treatment of wastewater solids and soluble organic material in accordance with the present invention; Figure lb is a schematic flow diagram of a three cell system for long or short hydraulic retention times to provide biological treatment of wastewater solids and soluble organic material in accordance with the present invention; Figure lc is a schematic flow diagram of a four cell system with two mirror image Figure la embodiments operating on an integrated basis in accordance with the present invention; Figure 2 is a schematic flow diagram of a four cell system for providing a higher treatment efficiency for difficult to treat wastewater in accordance with the present - 12 - SUBSTITUTESHEET i nvent ion ; Figure 3 is a schematic flow diagram of _ι six cell system suitable for also providing nitrogen removal in accordance with the present invention; Figure 4 is a schematic flow diagram of a six cell system suitable for also providing biological phosphorus as well as nitrogen removal in accordance with the present invention. Referring to Figure la, the most basic embodiment of the present invention includes two cells or zones in one basin capable of receiving constant inflow and maintaining a substantially constant operating level for long hydraulic retention time systems. The untreated wastewater may be continuously introduced into Cell 1 via inlet pipe 2 at inlet 3 and flow continually out of Cell 1 through free hydraulic connection( s) at 31 to treatment discharge cell 20. The treatment discharge cell 20 is hydraulically and may be always unhinderedly and freely connected to cell 1 at 31. Cell 20 also is preverably less t-han one-half and typically 25-40% or less of the volume of the total treatment system. To obtain the most effective operation of cell 20, the hydraulic connection 31 may be multiple openings or an opening across the entire width of cell 20 near the top or bottom water level as used in conventional clarifier influent distribution systems. Similarly, - 13 - SUBSTITUTESHEET discharge flow control means 31 would optimally remove treated wastewater across the entire width of cell 20. The treated wastewater is discharged on a continuing basis through flow control means 41 via outlet pipe 42 except for brief solids transfer and settling periods as discussed below. Flow control means 41 can be provided by flow control weir means as disclosed in applicant's co-pending United States patent application serial number 07/963,479, filed October 19, 1992, fixed level weirs and commercially available discharge flow control means or conventional control valves connected to discharge pipe 42. Because the invention operates at a substantially constant level the use of conventional fixed level weirs and flow control valves can be utilized, which reduces the capital cost and improves operations by requiring less moving equipment than necessary for variable level SBR decanters. The aeration mixing means 51 in cell 1 typically supplies the majority of the oxygen and mixing necessary to achieve complete biological treatment of the wastewater by contact of the untreated wastewater with the mixed liquor suspended solids recycled from cell 20. The aeration mixing means 51 in cell 1 operates continuously which makes possible higher aerator utilization than possible with SBR systems. The aeration mixing means 58 in cell 20 is shut off during discharge of treated wastewater out of the system by outlet pipe 42. In - 14 - SUBSTITUTESHEET order to achieve maximum wastewater treatment efficiency, the discharge out of cell 20 of partially treated wastewater received from cell 1 through 31 can be prevented by control of the length of time of discharge out of 41 and 45 so the lag time between the input and output of flow received in cell 20 is not exceeded. If lower treatment efficiency is acceptable, naturally said lag time can be exceeded as appropriate within the system operating limitations. When the mixed liquor suspended solids from cell 1 accumulate by settling in cell 20 sufficiently to require removal, the following operating steps are used: the discharge flow control means 41 is closed for a short period and the aeration mixing means 58 turned on by the central control unit (not shown). A variety of commercially available, programmable logic controllers ( PLC' s) can be used to control all operating steps of the process similar to the control units used for conventional SBR processes. After re-suspension of the mixed liquor suspended solids, a portion of the mixed liquor suspended solids in cell 20 and co-mingled partially treated wastewater are pumped through pipe 70 by solids transfer pump 71 back to cell 1 at inlet 72. This partial solids transfer ensures continuing high biological solids in cell 1 and sufficient biological solids remaining in cell 20 for additional polishing of partially treated wastewater transferred into - 15 - SUBSTITUTE SHEET cell 20 from cell 1 prior to once again discharging treated wastewater out of cell 20 by opening flow control means 41. The rate and duration of flow by transfer pump 71 is also selected to ensure that the accumulation of mixed liquor suspended solids in cell 20 is not too high to prevent effective treatment cycles to achieve a substantially constant water level as discussed below. An essential part of this step of the process is the mixing accomplished by aeration mixing means 58. It is rioted that for some applications with low oxygen demand in the final cell 20, the use of just mixing means in cell 20 is possible (e.g. aeration may be eliminated and just mixing means used to re- suspend the mixed liquor suspended solids). When sufficient mixed liquor suspended solids have been transferred out of cell 20 back to cell 1, solids transfer pump 71 is shut off by the central control unit, and aeration mixing means 58 remains on for a brief period if required to provide final batch polishing treatment for the partially treated wastewater in cell 20. At the completion of this final polishing treatment step in cell 20, the aeration mixing means 58 is shut off by the control unit, and cell 20 mixed liquor suspended solids are provided a predetermined pre-settling time prior to reopening of flow control means 41 and treated wastewater once again is discharged on a continuing basis out of the treatment system - 16 - SUBSTITUTE SHEET v ia 42 . The above steps are repeated in recurring cycles to provide continuous wastewater treatment as directed by the central control unit at regular time or flow volume intervals or when biological solids from cell 1 have accumulated sufficiently in cell 20 to require removal by transfer back to cell 1. The means to achieve a substantially constant level operation and minimize the head loss of wastewater flowing through the system for this embodiment is to use a high rate of solids transfer and flow through pump 71 so the duration of zero discharge through flow control means 41 is minimized. Typical transfer flow rates would be 3 to 6 or more times the average flow into the treatment system and discharge out of 41 would occur typically 70-80% of the time for this embodiment. Achieving a substantially constant operating level for Figure la embodiment of the invention is most effective for long hydraulic retention time systems. Level variations of less than 1 foot are desirable, and preferably less than 3 - 6 inches and optimally less than 1 - 2 inches in order to achieve the most efficient oxygen transfer rates, effective use of fixed mounted aerators and also mixed liquor suspended solids settling in the last cell during the long treated wastewater discharge periods of up to 90% of the - 17 - SUBSTITUTESHEET time each day. Substantially, constant operating levels are possible compared with typically 5 - 10 feet for SBR processes. However, for relatively short hydraulic retention time systems, e.g. retention times of less than approximately 24 hours, substantially constant level operation is not easily achieved by the basic embodiment of the invention as illustrated in Figure la. The means to essentially eliminate significant operating level fluctuations for any hydraulic retention time and also virtually eliminate the head loss of wastewater passing through the treatment system is to use a second treatment discharge cell as shown in Figure lb with a similar hydraulic connection means 131 and 132 to the treatment discharge cells 120 and 121 respectively, as for cell 20 connection to cell 1 at 31 in Figure la. Figure lb has similar aeration mixing, solids transfer and discharge flow control means as for the embodiment of Figure la. The second treatment discharge cell 121 operates with solids transfer at 180 through pump 181 and discharge to cell 101 at 182, and has identical operating steps as used for cell 20 in Figure la, except said second treatment discharge cell 121 discharges treated effluent through flow control means 141. The result of this second preferred embodiment is a continuous flow into the system inlet 102 and essentially equal flow out of the total treatment system through outlet. 145 at all times for long or short hydraulic retention time - 18 - SUBSTITUTE SHEET systems. another benefit of this embodiment is by use of two lower flow rate transfer pumps 171, 181 working alternat vely from the two last cells 120, 121, respectively, the rate of transfer of biological solids back to the previous cell 101 would be more consistent and hence the food to micro-organism ratio in prior cells 101 would also be more consistent. In combination these two factors result m a more controlled process unlike SBR variable process conditions and thus makes possible optimized treatment system design, operation, and consistently high treatment efficiency. All other operations means of Figure lb system and operating methods used are similar to the equivalent means and system methods of Figure la. Each equivalent means of operation is designated by the same number as that used in Figure la plus 100 i.e. 2 is 102, 3 is 103 etc., and for Figure 3, 2 is 302, 203 is 303, etc. and for Figure 4, 2 is 402, and 3 is 403, etc. Continuous discharge and constant operating level can also be achieved for long or short hydraulic detention time systems by using two (or more) identical Figure la complete systems operating in parallel, as shown in Figure lc. The treatment system means in Figure lc mirror image of Figure la embodiment are designated as cell 1' , as for cell 1 in Figure la, aeration mixing means 58' as for 58 in Figure la cell 1, - 19 - SUBSTITUTESHEET aeration mixing means 58 respectively and so on, for those components performing the same functions. The result of this third preferred embodiment is that each side of the system would operate with no flow out of one of the treatment discharge cells 20 or 20' during operation of the other parallel system's treatment discharge cell 20' , 20, respectively. To obtain maximum utilization of the aeration mixing means of this third preferred embodiment, untreated wastewater may be introduced constantly into each first cell and the solids may be transferred at least in part, from the last cells 20 and 20' to feed cells 1* and 1 respectively, through recycle system 83, 84, 85 and recycle system 83', 84', 85' , respectively, instead of only to the feed cells hydraulically connected in series to each discharge cell. Alternatively, a common wall valved hydraulic connection (not shown) between cell 1 and cell 1' can be used to maintain a constant untreated wastewater flow into cells 1 and 1' . This third embodiment also has the benefit of facilitating the operation of one parallel system independently during inspection or maintenance down time on the other parallel system. Using parallel systems would also make it possible to control the flow through the identical parallel embodiments of the invention by use of flow control means on the influent to each system instead of controlling the flow out of each system. This flow control method is suited for certain - 20 - SUBSTITUTE SHEET applications, however, has reduced aerator utilization factors and less precise discharge timing as a result of slowly reducing flows out of discharge cells after the influent flow is diverted. Another use of the invention which would be capable of continuous flow and constant operating level wouJd be to utilize at least two large, equal sized treatment discharge cells, operated identically as cells 120 and 121 above, and to feed untreated wastewater into a very small common hydraulically connected first feed cell. Such a use of the invention would not be most cost effective, however, because of the inefficiencies of utilizing only about 50. of the aeration mixing means at one time. Such inefficiencies could be largely eliminated, however, by use of a say 4 or more equal sized treatment discharge cells each used alternatively like cells 120 and 121, resulting in approximately 75% or more aeration mixing means utilization at one time. The system illustrated in Figure 2 is similar to the system of Figure lb, except that two cells 201 and 202 are provided with continuously operating aeration mixing means 251 and 252 respectively and have hydraulic connection means 231, 232 and 233 to allow wastewater to flow unhindered through the system to the (last) treatment discharge cells 220 and 221. This configuration of the invention makes - 21 - SUBSTITUTE SHEET possible similar operation as that illustrated in Figure lb but provides for a higher degree of treatment efficiency by improved plug flow characteristics if necessary based on specific wastewater characteristics and treatment objectives. If even higher degrees of treatment efficiency are required and even further plug flow characteristics would be helpful, several additional treatment cells can be provided in series with cells 201 and 202. The system illustrated in Figure 3 provides for removal of soluble and particulate contaminants but also makes possible high efficiency nitrogen removal by adapting conventional activated sludge nitrogen removal process concepts to achieve the specific additional benefits available by use of this invention. The principles of operation of this embodiment are similar to those illustrated in Figure lb and Figure 2, except that transfer of mixed liquor suspended solids and co-mingled partially treated nitrified wastewater from cell 320 back to prior treatment cells can be provided with preferably two solids transfer pumps. The 371 and 374 transfer pumps in Figure 3 transfer mixed liquor suspended solids and co-mingled partially treated wastewater in whatever ratio is required from cell 320 back to the first two cells 301 and 302 respectively, wherein the aeration means is turned off or reduced as required for the aeration mixing means 351 and SUBSTITUTESHEET 352 respectively. The resulting mixing means 351 and 352 thus provide little if any dissolved oxygen thus achieving anox c conditions of typically not more than 0.5 mg/1 of dissolved oxygen making possible biological dentrification of the wastewater in treatment cells 301 and 302 respectively. Alternatively, separate aeration means and mixing means can be provided in both these cells and used separately as required to achieve mixing and the dissolved oxygen concentration as required from time to time for optimized process operations. A lower degree of dentrification and process control can be achieved by eliminating recycle solids transfer pump 374 and/or treatment cell 302. Likewise for certain high nitrogen wastewaters, and for the requirement of higher degree of treatment efficiency, additional dentrification cells may be added beyond the two cells 301 and 302, and the aeration means and mixing means in subsequent treatment cells may be operated sequentially for improved dentrification. As for previous embodiments of the invention; a constant operating level and essentially zero head loss and constant inlet flow at 302 and outlet flow at 345 can be achieved as shown in Figure 3 embodiment by providing a second (last) treatment discharge cell 321 in addition to cell 320 and operating in a similar manner as for Figure lb and Figure 2 embodiments. A mirror image independently SUBSTITUTE SHEET operated parallel system can also be used as in Figure lc embodiment above to achieve a fully constant operating level . The system and operation of Figure 4 embodiment is similar to Figure 3 embodiment and operation except that. Figure 4 embodiment provides a preferred embodiment, of the invention which also achieves biological removal of phosphorus in addition to the removal of nitrogen, and treatment of soluble and particulate contaminants. Advanced activated sludge biological phosphorus removal process technologies, such as the University of Cape Town (UCT) process or the Modified UCT (MUCT) process, utilize pre- treat ent anaerobic contact cell(s) having a dissolved oxygen concentration of typically less than 0.1 mg/1, in series with anoxic dentrification cell(s) having a dissolved oxygen concentration of typically less than 0.5 mg/1 prior to aerobic treatment, nitrification, settling of mixed liquor suspended solids in dedicated clarifiers and return of the activated sludge to the anoxic cell(s) and a recycle from anoxic cell(s) to the first anaerobic cell. This invention also can make improved, more cost effective use of these or other biological phosphorus removal technology concepts as illustrated in the Figure 4 embodiment as follows: mixed liquor suspended solids transfer pump 474 recycles solids and co-mingled nitrified partially treated - 24 - SUBSTITUTESHEET wastewater from cell 420 at 473 to achieve dentrification in anoxic cell 402, v-.hιch is maintained at a dissolved oxygen concentration typically of less than 0.5 mg/1. Pump 477 provides for recycle of mixed liquor suspended solids and co-mingled dentrified partially treated wastewater from anoxic cell 402 at 476 to anaerobic cell 401 at 478 to optimize the operation of cell 401, which is maintained at dissolved oxygen concentrations of typically less than 0.1 mg/1. If greater treatment efficiency is required more cells can be used to increase the number of anaerobic, anoxic or even aerobic treatment cells as required. In addition selected cell aeration means and mixing means can be operated sequentially instead of continuously as required to improve the treatment efficiency of nutrient removal for all embodiments of the invention. Similar to the embodiments of the invention shown in Figures lb, 2 and 3, the system as shown in the Figure 4 embodiment can achieve a fully constant operating level and essentially zero head loss through the treatment system by providing a second (last) treatment discharge cell 421 to operate alternatively to cell 420 when no discharge is occurring through outlet flow control device 441. Other alternatives can also be used to achieve these objectives as discussed above. For dll embodiments of the invention, the necessary SUBSTITUTESHEET removal or wasting υf excess solids can be accomplished by pumping of mixed liquor suspended solids from an intermediate aerobic cell prior to the last cell(s) at a continuous rate as required to achieve the treatment system's desired sludge age. Alternatively, if pre- thickened settled sludge wasting is desired, intermittent wasting of excess solids can be achieved by pumping settled mixed liquor suspended solids from the (last) treatment discharge cell(s) during settling and solids accumulation steps utilizing conventional sludge collection systems. The result of use of the solids transfer pump(s) and the hydraulic connection means between the cells of all embodiments of the invention is a dynamic biological solids inventory and wastewater flow pattern that circulates around and through each system, but the concentrations of solids and wastewater patterns can be predicted in advance using conventional mass balance and flow simulation methods. Using these methods in combination with conventional process kinetic models makes possible solids management and accurate design predictions of treatment efficiency for any pre- characterized wastewaters treatable with conventional activated sludge processes. The net result of the present invention is a process and treatment system capable of achieving the most effective food to micro-organism ratio ranges in all treatment cells, - 26 - SUBSTITUTESHEET hence a consistently high treatment efficiency in a single basin, with a continuous flow single inlet, and constant or substantially constant discharge flow capabilities at typical medium operating depths of 10 - 30 feet. The system can productively utilize essentially all of the available land area and treatment systems volume 100% of the time, maintaining the process treatment benefits and eliminate the disadvantages of both the SBR and the conventional activated sludge processes. Finally the invention can reduce the capital cost and simplify operations of conventional treatment systems by eliminating separate dedicated clarification systems for the conventional activated sludge process and variable level flow control decanters for SBRs. These objectives can be met while maintaining substantially constant operating level with virtually no significant hydraulic head loss through the system, which is not possible with SBRs or even conventional activated sludge systems because of secondary clarifier head losses. The present invention also makes possible economical high efficiency biological removal of nutrients even for dilute or cool wastewaters. This often cannot be reliable achieved by SBR processes, which attempt to provide all treatment steps sequentially in one cell "instead of using separate high efficiency dedicated anaerobic and anoxic cells with optimized recycles. The present invention also SUBSTITUTESHEET accomplishes high efficiency nutrient removal without the use of the extra large dedicated final clarifiers typically required for conventional high efficiency activated sludge nutrient removal process systems. The present invention also makes possible the retrofit of existing aerated basins or lagoons to a higher treatment efficiency activated sludge style of treatment . by making possible virtually no head loss through the system and installation of retrofit baffles "on-the-run" to create the treatment discharge cells as specified for this invention without the necessity of shutting down the existing aerated basins or lagoons. Finally, the present invention has been shown to be capable of achieving higher aerator utilization ratios and diffuser oxygen transfer efficiency than possible with the SBR variable level process. Also possible are higher efficiency of aeration power use which does not exceed limiting power per unit volume factors. The system has been shown to be cost effective for low or high strength wastes, and for both small or large flows at low or high hydraulic retention times and low or high food to micro-organism ratios. Although the invention has been described as being intended for biological wastewater treatment systems, it will be appreciated that the invention could be used for other water or wastewater treatment applications such as - 28 - SUBSTITUTE SHEET chemical locculation and settling or anaerobic removal of contaminants, e.g. the anaerobic contact process as well as other biological, chemical, or other processes requiring reaction or treatment contact time with mixing or aeration followed by gravity t-larification of solids prior to recycle of solids and co-mingled treated or partially treated fluid during mixing of the final treatment cell to complete the process cycle. Having thus provided a general discussion, described the overall method and system in detail and illustrated the invention with typical examples and simple schematics of how to utilize the invention, it is now evident that effective solutions have been provided by the invention over operating and high cost problems of prior art. It is therefore to be understood that no undue restrictions are to be imposed by reason of the specific embodiments of the invention as illustrated and discussed herein. 29 - SUBSTITUTESHEET

Claims: THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS: 1. A method of treating water containing contaminants, comprising of the steps of: a) providing at least two hyd aulically connected treatment cells; b) introducing untreated water into at least the first of the at least two treatment cells for which said first cell is hydraulically connected to each treatment discharge cell; c) causing flow of water through the at least two cells; d) maintaining the level of water in at least the treatment discharge cell(s) at a substantially constant level; e) treating the water in each of the at least two cells; f) periodically mixing the water in each discharge cell so that previous settled solids will be resuspended; g) returning a portion of the water in each discharge cell back to a previous cell while discharge cell waters are being mixed in the previous mixing step; h) discharging treated water from said discharge oell(s) alternatively and only in the absence of water being mixed in the previous mixing step; - 30 - SUBSTITUTE SHEET 1) providing a central control for regulating the performance of the previous steps. 2. A method of treating water containing contaminants as defined in claim 1, further comprising the step of freely connecting said hydraulically connected treatment cells. 3. A method of continuously treating wastewater having soluble and particulate contaminants, comprising the steps of: a ) providing a first inlet cell for receiving and treating untreated wastewater; b) providing ._ first treatment discharge cell for final treatment and discharge of treated wastewater received from said first inlet cell; c) hydraulically connecting said first inlet cell with each treatment discharge cell; d) maintaining the level of wastewater substantially constant in at least all treatment discharge cells; e) introducing untreated wastewater into said first mlet cell; f) treating the wastewater by aerating and mixing the wastewater in said first cell for oxygenating and mixing mixed liquor suspended solids in said first inlet cell; g) periodically aerating and mixing wastewater in each treatment discharge cell for providing oxygen for additional treatment oτf partially treated wastewater and for resuspendmg and mixing the mixed liquor suspended solids; - 31 - SUBSTITUTE SHEET h) transferring back a portion of the wastewater in each treatment discharge cell to a previous cell during the steps of aerating and mixing treatment discharge cell wastewater; i ) discharging wastewater from said discharge cell(s) only in the absence of wastewater being mixed in said discharge cell (s) ; and j) providing a central control for regulating the performance of the previous steps. 4. A method of treating wastewater containing contaminants as defined in claim 3, further comprising the step of freely connecting said hydraulically connected treatment cells. 5. A method of treating wastewater as defined in claim 4, further comprising the steps of; a) providing a second treatment discharge cell; b) aerating and mixing wastewater in said second treatment discharge cell substantially concurrently with the stopping of aerating and mixing water in said first treatment discharge cell; and c) supplying wastewater from said first inlet cell to said second treatment discharge cell as well as continuing to supply wastewater from said first inlet cell to said first treatment discharge cell. 6. A method of treating wastewater as defined in claim 5, further comprising the steps of: - 32 - SUBSTITUTESHEET a) providing at least one additional treatment discharge cell; b) supplying wastewater from said first inlet cell to each said additional treatment discharge cell as well as '-ontinumg to supply wastewater from said first inlet cell to said first treatment discharge cell. 7. A system for continuously treating wastewater having soluble and particulate contaminants, comprising: a) a first inlet cell for receiving and treating untreated wastewater; b) a first treatment discharge cell for final treatment and discharge of treated wastewater received from said first inlet cell; c) said first inlet cell being hydraulically connected with all treatment discharge cells; d) means for maintaining the level of wastewater in at least all treatment dischέirge cell(s) substantially constant; e) means for introducing untreated wastewater into said first inlet cell; f) means for aerating and mixing the wastewater in said first inlet cell for oxygenating and mixing mixed liquor suspended solids in said first inlet cell; g) means for periodically aerating and mixing wastewater in each treatment discharge cell for providing oxygen for additional treatment of partially treated wastewater and for - 33 - SUBSTITUTE SHEET resuspending and mixing the mixed liquor suspended solids therein; h) means for transferring back a portion of the wastewater in each treatment discharge cell to a prior cell during mixing of treatment discharge cell wastewater; i) means for discharging treated wastewater out of each treatment discharge cell only in the absence of wastewater being mixed in each said discharge cell; and j) central control means for regulating the operation of the system. 8. A system of treating wastewater containing contaminants as defined in claim 7, wherein said first inlet cell is provided a means to be freely connected with all said hydraulically connected treatment cells. 9. A system for continuously treating wastewater as defined in claim 8, further comprising: a) at least one additional treatment discharge cell; and b) means for controlling the alternate discharge of treated wastewater out of said first and said at least one additional treatment discharge cell. 25 - 34 - SUBSTITUTESHEET

Inventors: TIMPANY PETER L, TIMPANY, PETER, L.
Applicants: TIMPANY PETER L, TIMPANY, PETER, L.
Application year: 1994
Main classification: C02F3
IPC codes: C02F3